U.S. patent number RE40,943 [Application Number 11/211,027] was granted by the patent office on 2009-10-27 for method in treating aqueous waste feedstream for improving the flux rates, cleaning and the useful life of filter media.
This patent grant is currently assigned to Diversified Technologies Services, Inc.. Invention is credited to Dennis A. Brunsell.
United States Patent |
RE40,943 |
Brunsell |
October 27, 2009 |
Method in treating aqueous waste feedstream for improving the flux
rates, cleaning and the useful life of filter media
Abstract
A method in treating aqueous feedstream in diverse plant site
environments is disclosed for improving filter flux rates, cleaning
filter media and prolonging useful operative life of media. In
preferred embodiments the method is provided with steps for
contacting, reacting, pressurizing and equalizing ozone and
feedstream within a central area or multiple areas and sustaining
high pressure throughout the system to achieve qualitatively and
quantitatively improved permeate products, and reject for recycle.
The method and system provide an improved cleaning and processing
system characterized by an ozone-concentrated, homogeneous single
phase liquid conversion of a generated ozone gas mixture and a
feedstream source containing organic and inorganic pollutants. The
method improves and monitors ozone oxidizing power and reflecting
ORP values, and provides further media cleaning and improved
oxidation reactions for attack on pollutants on each cycle/recycle
operation.
Inventors: |
Brunsell; Dennis A. (Knoxville,
TN) |
Assignee: |
Diversified Technologies Services,
Inc. (Knoxville, TN)
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Family
ID: |
29734144 |
Appl.
No.: |
11/211,027 |
Filed: |
August 24, 2005 |
Related U.S. Patent Documents
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Application
Number |
Filing Date |
Patent Number |
Issue Date |
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Reissue of: |
10176428 |
Jun 19, 2002 |
06755977 |
Jun 29, 2004 |
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Current U.S.
Class: |
210/648; 210/760;
210/797; 210/808 |
Current CPC
Class: |
C02F
1/78 (20130101); C02F 1/001 (20130101); C02F
1/444 (20130101); C02F 2301/066 (20130101); C02F
2209/04 (20130101); C02F 2209/23 (20130101); C02F
2201/782 (20130101) |
Current International
Class: |
C02F
1/78 (20060101); B01D 65/06 (20060101) |
Field of
Search: |
;210/746,760,791,797,805,808,648 ;422/186.08 |
References Cited
[Referenced By]
U.S. Patent Documents
Foreign Patent Documents
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57-194005 |
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Nov 1982 |
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JP |
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04-310220 |
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Nov 1992 |
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JP |
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2001-070764 |
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Mar 2001 |
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JP |
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2001-219165 |
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Aug 2001 |
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JP |
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Other References
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Water" GDT Web(http://www.gdt-h2o.com) Aug. 25, 1999, p. 3,
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Chelsea, Michigan. cited by examiner .
Drosie, R.I., 1997, Theory And Practice Of Water And Wastewater
Treatment, pp. 450-451 and 527-530, John Wiley & Sons; New
York. cited by examiner .
Mallevialle, J. et al., 1992, Influence and Removal of Organics in
Drinking Water, pp. 326-332, Lewis Publishers: Boca Raton. cited by
examiner .
Vigneswaren, D., et al., Water, Wastewater, and Sludge Filtration,
pp. 61-65, CRC Press, Inc.: Boca Raton, 1989. cited by examiner
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Faust, S.D. and Aly, O.M., 1998, Chemistry of Water Treatment, pp.
292-298, Ann Arbor Press: Chelsea, Michigan. cited by
examiner.
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Primary Examiner: Lawrence; Frank M
Attorney, Agent or Firm: Monroe Alex Brown Patent
Attorney
Claims
I claim:
1. A method for processing organic pollutants, and inorganic
foulants in a reduced oxidative state, of an aqueous feedstream,
increasing flux rates across a filtration membrane, and cleaning
and prolonging the useful life of filtration and filter membrane
installations, said method and system comprising: (a) directing,
channeling and pumping an aqueous feedstream having contaminants,
from a feed water area to a reactor area for contacting, reacting,
pressurizing and equalizing the aqueous feedstream, and
concentrating solids and removing solids from the aqueous
feedstream; (b) generating an ozone mixture having at least O.sub.3
and O.sub.2, dissolving the ozone mixture into the aqueous
feedstream under a pressure gradient having an alpha pressure,
contacting the aqueous feedstream with the ozone mixture such that
the aqueous feedstream is exposed for increased reaction of the
ozone and concentrating and collecting solids at a bottom portion
of said processing area; (c) directing the aqueous feedstream from
the reactor area and measuring ozone activity of the aqueous
feedstream; (d) conveying the aqueous feedstream to a pumping area;
(e) pumping the aqueous feedstream to a filtration area having a
filter media, an inflow portion subarea and an outflow portion
subarea, respectively, before and after the filter media; (f)
marshaling an effluent portion volume of the aqueous feedstream
passing through the filter media of the filtration area to the
outflow portion subarea, and advancing and measuring ozone activity
of the effluent portion volume, and the volume and amount of the
effluent portion volume; (g) advancing the effluent portion to a
preselected site.
2. The method of claim 1, wherein, after step (e): (e)(1)
marshaling a reject portion volume of the aqueous feedstream not
passing through the filter media, and proximal to the inflow
portion subarea of the filtration area and advancing the reject
portion volume to a recycle line.
3. The method of claim 2, wherein, after advancing the reject
portion volume to a recycle line: (e)(2) measuring ozone activity
of the reject portion volume.
4. The method of claim 3, further comprising: (e)(3) channeling the
reject portion volume to the reactor area, and adding a further
aqueous feedstream volume from the feed water area equal in volume
and amount to that of the effluent portion volume, thereby, forming
a new aqueous feedstream volume.
5. The method of claim 4, wherein, after step (e)(3): recycling the
new aqueous feedstream volume through steps (b), (c), (d), (e), (f)
and (g); and steps (e)(1), (e)(2) and (e)(3).
6. The method of claim 2, wherein the alpha pressure is equal to
from about 10 p.s.i.g. to about 150 p.s.i.g.
7. The method of claim 6, wherein, in the generating of step (b)
the ozone mixture is provided by an ozone generator at an output of
from about 1 p.s.i.g. to about 150 p.s.i.g.
8. The method of claim 6, wherein step (b) further comprises
supplying the aqueous feedstream to an area over water where the
ozone mixture is generated and interfaced with the alpha pressure
being equal to from about 30 p.s.i.g. to about 50 p.s.i.g.
9. The method of claim 6, wherein, in step (b), the alpha pressure
is equal to from about 100 p.s.i.g. to about 2000 p.s.i.g.
10. The method of claim 6, wherein, step (b) further comprises
channeling the aqueous feedstream, to a positioned area having an
upper level surfacing, under the alpha pressure, and generating the
ozone mixture at a positioning relative to the aqueous feedstream
such that it passes throughout the aqueous feedstream to the upper
level surfacing.
11. The method of claim 6, wherein, dissolving the ozone mixture
into the aqueous feedstream under the pressure gradient having the
alpha pressure, comprises solubilizing the ozone mixture and the
aqueous feedstream such that a substantially homogeneous single
phase liquid mixture is formed whereby the ozone mixture and the
aqueous feedstream are dissolved and miscible, one with the other,
at a level below the saturation point of the ozone mixture.
12. A process for removing and destroying organic foulants and
inorganic foulants in a reduced oxidative state, applied in
utilization upstream of filtration membranes, for increasing flux
rates and prolonging the useful life of filter membranes, said
process and system comprising: (a) directing and channeling an
aqueous feedstream from a site waste water area to a dissolving
area; (b) generating an ozone mixture having at least O.sub.3 and
O.sub.2, and dissolving the mixture into the aqueous feedstream
under a pressure gradient having an alpha pressure, such that the
mixture having at least O.sub.3 and O.sub.2 is dissolved and
miscible within the aqueous feedstream at a level below saturation
point and the ozone mixture and the aqueous feedstream are
solubilized to produce a substantially homogeneous single phase
mixture; (c) channeling the aqueous feedstream to a
contact-surfacing enhancement area; (d) contacting and surfacing
the aqueous feedstream by slowing the aqueous feedstream and
providing additional surface area for the occurrence of further
oxidation reactions and destruction of organic and other substrates
detrimental to filter membranes; (e) directing the aqueous
feedstream from the contact-surfacing enhancement area and
measuring ozone activity of the aqueous feedstream; (f) conveying
the aqueous feedstream to a back pressure valve and maintaining
pressure; (g) transporting the aqueous feedstream to a recycle tank
area, and concentrating and collecting solids at a bottom portion
thereof; (h) moving the aqueous feedstream into a pumping area; (i)
repressurizing the aqueous feedstream to the alpha pressure and
pumping the aqueous feedstream to a filter membrane area having a
filter media, an inflow portion and an outflow portion,
respectively, in front of and beyond the filter media; (j)
marshaling an effluent portion of the aqueous feedstream passing
through the filter membrane area to the outflow portion and
advancing and measuring the effluent portion for ozone activity and
volume amount; and (k) advancing the effluent portion to a
preselected site.
13. The process of claim 12, wherein, after step (i): marshaling a
reject portion of the aqueous feedstream not passing through the
filter, proximal to the inflow portion of the filter membrane area,
and advancing the reject portion to a recycle line.
14. The process of claim 13, wherein: after advancing the reject
portion to a recycle line, measuring ozone activity and volume
amount, and directing the reject portion back to the recycle tank
area of step (g).
15. The process of claim 14, wherein, at selected time sequences,
cleaning the recycle tank area and evacuating solids and like fluid
substances from the bottom portion of the recycle tank area, and
transporting the solids and like fluid substances to the site waste
water area.
16. The process of claim 12, wherein: the alpha pressure is equal
to from about 10 p.s.i.g. to about 150 p.s.i.g.
17. The process of claim 16, wherein: the alpha pressure is equal
to from about 30 p.s.i.g. to about 50 p.s.i.g.
18. The process of claim 12, wherein: the alpha pressure is equal
to from about 100 p.s.i.g. to about 2000 p.s.i.g.
19. The process of claim 16, wherein, in the generating of step
(b), the ozone mixture is provided by an ozone generator at an
output of at least from about 1 p.s.i.g. to about 150 p.s.i.g.
20. The process of claim 12, wherein, after step (b) and before
step (c): channeling the aqueous feedstream and measuring ozone
activity of the aqueous feedstream.
21. The process of claim 12, wherein: the dissolving of step (b)
further comprises exposing the aqueous feedstream to water-leveling
by virtue of a water level means, for preventing the ozone mixture
from leaving the aqueous feedstream.
22. The method of claim 5, wherein: an ORP data result in mV units
is obtained from the step (c), and utilized on the recycling of the
new aqueous feedstream volume, so as to adjust the generating of
step (b) to a rate of ozone output where the aqueous feedstream in
step (b) in the recycling of the new aqueous feedstream volume is
from about 750 mV. to about 800 mV.
.Iadd.23. A method for cleaning a filter installation, where the
filter is in an installed position on line and used for
environmental filtering of a wastestream, and respective volumes
thereof from respective source areas of the wastestream, having
fluid contaminants generated by at least one of respective
manufacturing and nuclear work facilities; wherein said fluid
contaminants having at least one of respective organic and
inorganic pollutants, contaminants and foulants, and hazardous and
contaminating chemicals, substances or matter; and comprising a
system of conveyance, under continuing, monitored pressure, for
forward and frontal entry and passage through the filter
installation to be cleaned of a homogeneous cleaning fluid or
portions thereof; said method further comprising the steps of
directing the wastestream, and the respective volume thereof, from
the respective source area of the wastestream to a processing area
for oxidation of the fluid contaminants; homogeneously dissolving
and solutionizing an ozone gas volume into the wastestream under a
pressure gradient, such that the wastestream becomes the
homogeneous cleaning fluid, said cleaning fluid being a
substantially single phase fluid; verifiably measuring the ozone
activity in the cleaning fluid after leaving the processing area,
proximate to at least one point of respective points extending to
and beyond the filter to be cleaned; and selectively making
adjustments to the pressure exerted in the processing area and the
ozone gas volume supplied to the processing area during an on-going
cycle, and recycling and adjusting wastestream volumes and any
volumes of the cleaning fluid not passing through the filter to be
cleaned back to the processing area, thereby reducing ozone bubbles
and white water therefrom in the wastestream and cleaning fluid as
it is directed in the system of conveyance from within the
processing area to the filter installation to be
cleaned..Iaddend.
.Iadd.24. The method of claim 23, wherein, said cleaning fluid
becomes a substantially single phase liquid containing a small
quantity of suspended solids or particulates; with, generally, most
of the ozone gas volume being in solution..Iaddend.
.Iadd.25. The method of claim 23, wherein the cleaning fluid being
a substantially single phase liquid fluid; where the fluid
contaminants existing in the wastestream, and affected by the ozone
gas volume, produce substantially no solids for
removal..Iaddend.
.Iadd.26. The method of claim 23, wherein, prior to the step of
directing the wastestream to a processing area, the method further
comprising the step of measuring the oxidation reduction potential
of the wastestream..Iaddend.
.Iadd.27. The method of claim 23, further comprising the step of
measuring the oxidation reduction potential of the wastestream
while it is present in the processing area..Iaddend.
.Iadd.28. The method of claim 23, wherein, in the step of
homogeneously dissolving and solutionizing an ozone gas volume into
the wastestream, the method further comprising the use of an
eductor means to create a nozzle-type effect in introducing the
ozone gas volume into the wastestream from a position above said
wastestream..Iaddend.
.Iadd.29. The method of claim 23, wherein, between the source area
and the processing area, the step of measuring the ozone
activity..Iaddend.
.Iadd.30. The method of claim 24, wherein, generally
contemporaneous with the homogeneously dissolving and solutionizing
step, collecting at least part of any existing solids or solid-like
substances and particulates in the wastestream when
present..Iaddend.
.Iadd.31. The method of claim 23, wherein the step of making
adjustments further comprises selectively recycling and
communicating the cleaning fluid, or portions thereof, back to the
processing area for adding additional wastestream volumes from the
source and further dissolving and solutionizing with ozone gas
volumes..Iaddend.
.Iadd.32. The method of claim 23, wherein said method further
comprises generating an effluent portion volume after the forward
entry and passage through the filter installation to be cleaned of
the homogeneous cleaning fluid..Iaddend.
.Iadd.33. The method of claim 23, wherein said processing area
comprises at least one reactor area for contacting the wastestream
and ozone gas volume during the step of homogeneously dissolving
and solutionizing the ozone gas volume into the
wastestream..Iaddend.
.Iadd.34. The method of claim 33, wherein said at least one reactor
area comprises at least one member, selected from a group
consisting of: a chamber, a reservoir, a vessel, a column, a hose,
a pipe, a tube, and other means for contacting and solutionizing
the ozone gas volume with the wastestream such that the wastestream
becomes the homogeneous cleaning fluid..Iaddend.
.Iadd.35. The method of claim 33, wherein said processing area
comprises: a dissolving area for receiving the wastestream directed
and conveyed from the source area, for mixing and homogeneously
dissolving the ozone volume generated and provided with the
wastestream to said dissolving area; a reactor area for providing
structure and positionally arranged surfacing to expose the
wastestream to increased surfacing for greater oxidation by the
ozone gas volume dissolved in the wastestream; and a selectively
engageable recycle tank for concentrating any solids forming a part
of the wastestream and making them available for removal at a
preselected time from said recycle tank..Iaddend.
.Iadd.36. The method of claim 23, wherein, after verifiably
measuring the ozone activity in the cleaning fluid after leaving
the processing area, and at points prior to reaching the filter to
be cleaned, the step of selectively recycling, and conveying, the
cleaning fluid, or portions thereof, back to the processing
area..Iaddend.
.Iadd.37. The method of claim 23, wherein the pressure gradient is
from about 10 p.s.i.g. to about 2000 p.s.i.g..Iaddend.
.Iadd.38. The method of claim 32, further comprising, in addition
to measuring the ozone activity in the cleaning fluid becoming the
effluent portion volume at a point beyond the filter to be cleaned,
the step of advancing and measuring volume or amount of the
effluent portion volume after being generated..Iaddend.
.Iadd.39. The method of claim 32, further comprising the step of
advancing and measuring ozone activity of an effluent portion
volume of the cleaning fluid in contemporaneous relation to the
time period during which said effluent portion volume passes
through said filter installation to be cleaned..Iaddend.
.Iadd.40. The method of claim 32, further comprising the step of
marshaling an effluent portion volume of the cleaning fluid passing
through the filter installation to an outflow portion subarea, and
advancing and measuring ozone activity of the effluent portion
volume, and the volume and amount of the effluent portion
volume..Iaddend.
.Iadd.41. The method of claim 40, further comprising the step of
marshaling a reject portion volume of the cleaning fluid not
passing through the filter installation, proximal to a inflow
portion subarea of the filter installation, and advancing and
conveying the reject portion volume to the processing
area..Iaddend.
.Iadd.42. The method of claim 41, wherein, before the reject
portion volume reaches the processing area, measuring ozone
activity of the reject portion volume..Iaddend.
.Iadd.43. The method of claim 41, further comprising the step,
generally contemporaneous with said advancing and conveying the
reject portion volume to the processing area, of adding a further
volume of wastestream from the respective source area of the
wastestream equal in volume and amount to that of the effluent
portion volume; thereby, forming a new wastestream volume for
processing..Iaddend.
.Iadd.44. The method of claim 23, wherein the processing area of
said directing step being an area over water, and where the step of
homogeneously dissolving and solutionizing an ozone volume into the
wastestream is conducted with the pressure gradient being equal to
from about 10 p.s.i.g. to about 2000 p.s.i.g..Iaddend.
.Iadd.45. A method for processing organic and inorganic fluid
contaminants in an aqueous feedstream and cleaning an
environmentally efficacious filter media installation, serving at
least one of respective municipal, manufacturing and nuclear
facilities generating the fluid contaminants in the feedstream,
comprising the steps of conveying the feedstream to a dissolving
area; generating an ozone volume having O sub. 3 and O sub. 2, and
homogeneously dissolving and solutionizing the ozone volume into
the feedstream under a pressure gradient to affect the feedstream
by forming a single phase ozone-feedstream mixture volume
therewithin; communicating the feedstream to a contact-surfacing
enhancement area; measuring ozone activity; selectively making
adjustments to the feedstream; conveying the feedstream through the
filter media installation and generating an effluent portion
volume; and advancing and measuring ozone activity of the effluent
portion volume, and the volume and amount of the effluent portion
volume..Iaddend.
.Iadd.46. The method of claim 45, further comprising generating a
reject portion volume from the feedstream not passing through the
filter installation..Iaddend.
.Iadd.47. The method of claim 46, further comprising measuring
ozone activity of the reject portion volume and recycling said
reject portion volume back to the dissolving area..Iaddend.
.Iadd.48. A method of cleaning a filter installation, where the
filter installation is in position and used for environmentally
filtering organic and inorganic wastestreams, and respective
wastestream volumes thereof, generated by at least one of
respective manufacturing and nuclear activities and facilities, and
respective wastestream sources thereof, comprising providing a
system of conveyance to the filter installation of a volume of a
substantially homogenized cleaning fluid and frontal entry and
passage through said filter installation of a portion of the volume
of the substantially homogenized cleaning fluid, thereby cleaning
said filter, said cleaning fluid containing an oxidizing ozone gas
volume having O3 and O2 and the wastestream volume; maintaining the
ozone gas volume under verifiably tested pressure and amount within
the cleaning fluid such that it is so maintained throughout the
system, with the wastestream, to the filter installation and the
frontal entry and passage through said filter installation of the
portion of the cleaning fluid; wherein, said filter installation is
selected from a group of units consisting of: cross flow and
tubular filtration units, ultrafiltration membrane systems, filters
used for radioactive liquids, precoat filters, septum filters,
flatbed filters, centrifugal filters, etched disk filters, deep-bed
filters, clam shell filters, magnetic filters, sand filters and
other filters specifically related to cleaning wastestream products
as a result of manufacturing or radiation activities; regularly and
systematically testing the cleaning fluid for ORP, and adjusting
the pressure and amount of the ozone gas volume in accordance with
the ORP readings such that the cleaning fluid is maintained in
conveyance within the system in a sufficiently oxidized state for
cleaning the filter installation upon said frontal entry and
passage through the filter installation of the portion of the
cleaning fluid; and conveying the cleaning fluid to the filter
installation and generating an effluent portion volume from the
portion of the cleaning fluid being so conveyed by the frontal
entry and passage through said filter installation..Iaddend.
.Iadd.49. The method of claim 48, wherein the cleaning fluid is
substantially a single phase liquid having or containing a small
quantity or amount of suspended solids, with most of the ozone gas
being in solution, and maintained in that condition throughout the
system by said testing of the cleaning fluid for ORP..Iaddend.
.Iadd.50. The method of claim 48, further comprising the steps of:
(a) directing the respective wastestream volume from the respective
wastestream source to a processing area for ozone mixture and
oxidation; (b) homogeneously dissolving and solutionizing the ozone
gas volume into the wastestream volume under a pressure gradient to
form the volume of the cleaning fluid; and (c) conveying the volume
of the cleaning fluid, while maintaining the pressure gradient, to
the filter installation for the frontal entry and passage through
said filter installation of the portion of the volume of the
cleaning fluid and direct cleaning of the filter
installation..Iaddend.
.Iadd.51. The method of claim 50, further comprising the step of
generating a reject portion volume comprising that part of the
cleaning fluid not passing through the filter
installation..Iaddend.
.Iadd.52. The method of claim 51, further comprising the steps of
measuring the amount of the effluent portion volume; and directing
the reject portion volume to the processing area..Iaddend.
.Iadd.53. The method of claim 52, further comprising the step of
adding an amount of additional wastestream from the wastestream
source, proportional to the amount of the effluent portion volume;
and repeating steps (a), (b) and (c)..Iaddend.
.Iadd.54. The method of claim 51, further comprising the step of
adding an amount of additional wastestream in step (a),
proportional to the amount of effluent portion volume..Iaddend.
.Iadd.55. The method of claim 50, further comprising the step of
adding an amount of additional wastestream volume proportional to
the amount of the cleaning fluid passing through the filter
installation..Iaddend.
.Iadd.56. The method of claim 48, further comprising the steps of:
conveying the wastestream volume from the wastestream source to a
dissolving area; homogeneously dissolving and solutionizing the
ozone gas volume with the wastestream volume, in said dissolving
area, under a pressure gradient; and directing the wastestream
volume to a reactor area for providing structurally and
positionally disposed surfacing areas to expose the wastestream
volume to increased oxidation availability, and mixing and
solubilizing of the ozone gas volume with the wastestream volume,
such that the cleaning fluid is formed for passing through said
filter installation..Iaddend.
.Iadd.57. The method of claim 56, further comprising between the
step of homogeneously dissolving and solutionizing the ozone gas
volume and the step of directing the wastestream volume to a
reactor area; the step of testing or verifiably measuring the
wastestream volume for ozone content..Iaddend.
.Iadd.58. The method of claim 56, wherein, proximate to or within
said reactor area, selectively and optionally separating and
collecting at least part of any solid or particular organic
contaminants existing in the wastestream volume, when such
contaminants exist therein..Iaddend.
.Iadd.59. The method of claim 48, further comprising the steps of:
conveying the wastestream volume from a source to a dissolving
area; homogeneously dissolving and solutionizing the ozone volume
with the wastestream volume, in said dissolving area, under a
pressure gradient; directing the wastestream volume, so treated, to
a reactor area for providing structurally and positionally disposed
surfacing to expose the wastestream volume to increased surfacing,
positioning and exposure of various internal and external volume
portions thereof, for greater oxidation by the ozone volume
dissolved and solutionized in the wastewater volume; thereby
forming the cleaning fluid; selectively moving the cleaning fluid
to a recycle tank area for concentrating any solid and particular
contaminants, when existing and forming a part thereof, and making
the solid and particulate contaminants available for removal at a
preselected time from the recycle tank area; and directing the
cleaning fluid to the filter installation..Iaddend.
.Iadd.60. The method of claim 50, wherein the pressure gradient is
achieved by means selected from a group consisting of: providing
the wastestream volume to the processing area under pressure,
providing the ozone gas volume to the processing area under
pressure, and providing both the wastestream volume and the ozone
gas volume to the processing area under pressure..Iaddend.
.Iadd.61. The method of claim 59, further comprising the step of
generating a reject portion volume comprising that part of the
cleaning fluid not passing through the filter
installation..Iaddend.
.Iadd.62. The method of claim 61, wherein, the reject portion
volume comprising that part of the cleaning fluid not passing
through the filter installation is conveyed for rejection or
exiting from the system of conveyance of the method..Iaddend.
.Iadd.63. The method of claim 23, wherein a necessary item of
equipment, or system utilized to facilitate the steps of the
present method are sized and adjusted with regard to its
specifications or limits of structural makeup and functional use,
so as to be able to accommodate the magnitude, volume and nature of
the wastestream and cleaning fluid of said method..Iaddend.
.Iadd.64. A method for processing fluid contaminants containing
organic and inorganic pollutants and foulants or other contaminants
in an aqueous feedstream, comprising the steps of directing the
feedstream to a processing area for oxidation of the fluid
contaminants; homogeneously dissolving and solutionizing an ozone
gas volume into the feedstream, such that the feedstream becomes a
substantially single phase fluid; measuring ozone activity in the
feedstream after leaving the processing area; selectively and
optionally making adjustments to the feedstream based on the
results of the measuring step; delivering the feedstream to a
filtration area for direct passage therethrough; and marshaling an
effluent portion volume of the feedstream passing through the
filtration area to an outflow portion subarea, and advancing and
measuring ozone activity of the effluent portion volume, and the
volume and amount of the effluent portion volume..Iaddend.
.Iadd.65. A method for processing fluid contaminants containing
organic and inorganic pollutants and foulants or other contaminants
in an aqueous feedstream, comprising the steps of directing the
feedstream to a processing area for oxidation of the fluid
contaminants; homogeneously dissolving and solutionizing an ozone
gas volume into the feedstream, such that the feedstream becomes a
substantially single phase fluid; measuring ozone activity in the
feedstream after leaving the processing area; selectively and
optionally making adjustments to the feedstream based on the
results of the measuring step; delivering the feedstream to a
filtration area for direct passage therethrough; and marshaling a
reject portion volume of the feedstream not passing through the
filtration area, proximal to a inflow portion subarea of the
filtration area, and advancing the reject portion volume to a
recycle line for return to the processing area..Iaddend.
.Iadd.66. A method for processing fluid contaminants containing
organic and inorganic pollutants and foulants or other contaminants
in an aqueous feedstream, comprising the steps of directing the
feedstream to a processing area for oxidation of the fluid
contaminants; homogeneously dissolving and solutionizing an ozone
gas volume into the feedstream, such that the feedstream becomes a
substantially single phase fluid; measuring ozone activity in the
feedstream after leaving the processing area; and selectively and
optionally making adjustments to the feedstream based on the
results of the measuring step; delivering the feedstream to a
filtration area for direct passage therethrough; marshaling a
reject portion volume of the feedstream not passing through the
filtration area, proximal to a inflow portion subarea of the
filtration area, and advancing the reject portion volume to a
recycle line for return to the processing area; and, after
advancing the reject portion volume to a recycle line, and before
reaching the processing area, measuring ozone activity of the
reject portion volume..Iaddend.
.Iadd.67. A method for processing fluid contaminants containing
organic and inorganic pollutants and foulants or other contaminants
in an aqueous feedstream, comprising the steps of directing the
feedstream to a processing area for oxidation of the fluid
contaminants; homogeneously dissolving and solutionizing an ozone
gas volume into the feedstream, such that the feedstream becomes a
substantially single phase fluid; measuring ozone activity in the
feedstream after leaving the processing area; and selectively and
optionally making adjustments to the feedstream based on the
results of the measuring step; delivering the feedstream to a
filtration area for direct passage therethrough; marshaling a
reject portion volume of the feedstream not passing through the
filtration area, proximal to a inflow portion subarea of the
filtration area, and advancing the reject portion volume to a
recycle line for return to the processing area; and channeling the
reject portion volume to the processing area, and adding a further
aqueous feedstream volume equal in volume and amount to that of the
effluent portion volume; thereby, forming a new aqueous feedstream
volume..Iaddend.
.Iadd.68. A method of accomplishing an upstream
efficiency-enhancing treatment and cleaning of a filter
installation by providing for direct passage through said filter
installation of a single-phase homogenized ozoneaqueous solution,
comprising an ozone gas volume having O3 and O2, and a wastewater
volume, having contaminants; each solubilized and miscible, one
with the other, such that the wastewater volume is oxidized; and
further comprising the steps of: directing the wastewater volume,
having organic contaminants, from a source to a processing area for
ozone mixture and oxidation, homogeneously dissolving and
solutionizing the ozone gas volume into the wastewater volume under
a pressure gradient to form the single-phase homogenized
ozoneaqueous solution, directing the single-phase homogenized
ozoneaqueous solution, while maintaining the pressure gradient, to
the filter installation for passage therethrough and direct
cleaning thereof, and producing an effluent portion volume, after
passage of part of the single-phase homogenized ozoneaqueous
solution through the filter installation, and a reject portion
volume of that part of the single-phase homogenized ozoneaqueous
solution not passing through the filter installation..Iaddend.
.Iadd.69. A method of accomplishing an upstream
efficiency-enhancing treatment and cleaning of a filter
installation by providing for direct passage through said filter
installation of a single-phase homogenized ozoneaqueous solution,
comprising an ozone gas volume having O3 and O2, and a wastewater
volume, having contaminants; each solubilized and miscible, one
with the other, such that the wastewater volume is oxidized; and
further comprising the steps of: directing the wastewater volume,
having organic contaminants, from a source to a processing area for
ozone mixture and oxidation, homogeneously dissolving and
solutionizing the ozone gas volume into the wastewater volume under
a pressure gradient to form the single-phase homogenized
ozoneaqueous solution, and directing the single-phase homogenized
ozoneaqueous solution, while maintaining the pressure gradient, to
the filter installation for passage therethrough and direct
cleaning thereof, producing an effluent portion volume, after
passage of part of the single-phase homogenized ozoneaqueous
solution through the filter installation, and a reject portion
volume of that part of the single-phase homogenized ozoneaqueous
solution not passing through the filter installation, and measuring
the amount of the effluent portion volume; and directing the reject
portion volume to the processing area..Iaddend.
.Iadd.70. A method of accomplishing an upstream
efficiency-enhancing treatment and cleaning of a filter
installation by providing for direct passage through said filter
installation of a single-phase homogenized ozoneaqueous solution,
comprising an ozone gas volume having O3 and O2, and a wastewater
volume, having contaminants; each solubilized and miscible, one
with the other, such that the wastewater volume is oxidized; and
further comprising the steps of: (a) directing the wastewater
volume, having organic contaminants, from a source to a processing
area for ozone mixture and oxidation, (b) homogeneously dissolving
and solutionizing the ozone gas volume into the wastewater volume
under a pressure gradient to form the single-phase homogenized
ozoneaqueous solution, (c) directing the single-phase homogenized
ozoneaqueous solution, while maintaining the pressure gradient, to
the filter installation for passage therethrough and direct
cleaning thereof, (d) producing an effluent portion volume, after
passage of part of the single-phase homogenized ozoneaqueous
solution through the filter installation, and a reject portion
volume of that part of the single-phase homogenized ozoneaqueous
solution not passing through the filter installation, (e) measuring
the amount of the effluent portion volume; and directing the reject
portion volume to the processing area, and (f) adding an amount of
additional wastewater volume from the source, proportional to the
amount of the effluent portion volume; and repeating steps (a), (b)
and (c)..Iaddend.
.Iadd.71. A method of accomplishing an upstream
efficiency-enhancing treatment and cleaning of a filter
installation by providing for direct passage through said filter
installation of a single-phase homogenized ozoneaqueous solution,
comprising an ozone gas volume having O3 and O2, and a wastewater
volume, having contaminants; each solubilized and miscible, one
with the other, such that the wastewater volume is oxidized; and
further comprising the steps of: (a) directing the wastewater
volume, having organic contaminants, from a source to a processing
area for ozone mixture and oxidation, (b) homogeneously dissolving
and solutionizing the ozone gas volume into the wastewater volume
under a pressure gradient to form the single-phase homogenized
ozoneaqueous solution, and (c) directing the single-phase
homogenized ozoneaqueous solution, while maintaining the pressure
gradient, to the filter installation for passage therethrough and
direct cleaning thereof, (d) producing an effluent portion volume,
after passage of part of the single-phase homogenized ozoneaqueous
solution through the filter installation, and a reject portion
volume of that part of the single-phase homogenized ozoneaqueous
solution not passing through the filter installation; and (e)
adding an amount of additional wastewater volume in step (a),
proportional to the amount of effluent portion volume..Iaddend.
.Iadd.72. A method of accomplishing an upstream
efficiency-enhancing treatment and cleaning of a filter
installation by providing for direct passage through said filter
installation of a single-phase homogenized ozoneaqueous solution,
comprising an ozone gas volume having O3 and O2, and a wastewater
volume, having contaminants; each solubilized and miscible, one
with the other, such that the wastewater volume is oxidized; and
further comprising the steps of: conveying the wastewater volume
from a source to a dissolving area; homogeneously dissolving and
solutionizing the ozone volume with the wastewater volume, in said
dissolving area, under a pressure gradient, directing the
wastewater volume, so treated, to a reactor area for providing
structurally and positionally disposed surfacing to expose the
wastewater volume to increased surfacing, positioning and exposure
of various internal and external volume portions thereof, for
greater oxidation by the ozone volume dissolved and solutionized in
the wastewater volume; thereby forming the single-phase homogenized
ozoneaqueous solution, selectively and optionally moving the
single-phase homogenized ozoneaqueous solution to a recycle tank
area for concentrating any solid and particulate contaminants, when
existing and forming a part thereof, and making the solid and
particulate contaminants available for removal at a preselected
time from the recycle tank area, and directing the single-phase
homogenized ozoneaqueous solution to the filter installation for
passage therethrough..Iaddend.
.Iadd.73. A method of cleaning a filter installation, where the
filter installation is in position and used for environmentally
filtering a wastestream, said wastestream having at least one of
respective organic and inorganic pollutants, contaminants, foulants
and hazardous chemicals or substances, and a respective wastestream
volume thereof, generated by at least one of respective
manufacturing and nuclear activities and facilities; comprising:
providing a system of conveyance to the filter installation of a
volume of a substantially homogenized cleaning fluid and frontal
entry and passage through said filter installation of a portion of
the volume of the substantially homogenized cleaning fluid, thereby
cleaning said filter, said cleaning fluid containing an oxidizing
ozone gas volume having O3 and O2 and the wastestream; maintaining
the ozone gas volume under verifiably tested pressure and amount
within the cleaning fluid such that it is so maintained throughout
the system, with the wastestream, to the filter installation and
the frontal entry and passage through said filter installation of
the portion of the cleaning fluid; wherein, said filter
installation is selected from a group of units consisting of: cross
flow and tubular filtration units, ultrafiltration membrane
systems, filters used for radioactive liquids, precoat filters,
septum filters, flatbed filters, centrifugal filters, etched disk
filters, deep-bed filters, clam shell filters, magnetic filters,
sand filters and other filters specifically related to cleaning
wastestream products as a result of manufacturing or radiation
activities; regularly conducting at least one of respective
measurements or samplings of ozone content of the cleaning fluid
and readings and testings of the cleaning fluid for ORP; and
adjusting the pressure and amount of the ozone gas volume in
accordance with the at least one of the respective measurements of
ozone content and readings for ORP such that the cleaning fluid is
maintained in conveyance within the system in a sufficiently
oxidized state for cleaning the filter installation upon said
frontal entry and passage through the filter installation of the
portion of the cleaning fluid; and conveying the cleaning fluid to
the filter installation and generating an effluent portion volume
from the portion of the cleaning fluid being so conveyed by the
frontal entry and passage through said filter installation; and
wherein a necessary item of equipment, or system utilized to
facilitate the steps of said method are sized and adjusted with
regard to its specifications or limits of structural makeup and
functional use, so as to be able to accommodate the magnitude,
volume and nature of said wastestream and said oxidizing ozone gas
volume..Iaddend.
.Iadd.74. A method for processing fluid contaminants containing
organic and inorganic pollutants and foulants or other contaminants
in an aqueous feedstream, comprising the steps of directing the
feedstream to a processing area for oxidation of the fluid
contaminants; homogeneously dissolving and solutionizing an ozone
gas volume into the feedstream, such that the feedstream becomes a
substantially single phase fluid; measuring ozone activity in the
feedstream after leaving the processing area; selectively and
optionally making adjustments to the feedstream based on the
results of the measuring step; conveying the single phase fluid
through a filter media installation and generating an effluent
portion volume; and advancing and measuring ozone activity of the
effluent portion volume, and the volume and amount of the effluent
portion volume..Iaddend.
.Iadd.75. A method for cleaning a filter installation, where the
filter is in an installed position on line and used for
environmental filtering of a wastestream, and respective volumes
thereof from respective source areas of the wastestream, having
fluid contaminants generated by at least one of respective
manufacturing and nuclear work facilities, and comprising a system
of conveyance, under continuing, monitored pressure, for forward
and frontal entry and passage through the filter installation to be
cleaned of a homogeneous cleaning fluid or portions thereof; said
method further comprising the steps of directing the wastestream,
and the respective volume thereof, from the respective source area
of the wastestream to a processing area for oxidation of the fluid
contaminants; homogeneously dissolving and solutionizing an ozone
gas volume into the wastestream under pressure, such that the
wastestream becomes the homogeneous cleaning fluid, said cleaning
fluid being a substantially single phase fluid; verifiably
measuring the ozone activity in the cleaning fluid after leaving
the processing area, proximate to at least one point of respective
points extending to and beyond the filter to be cleaned; and
selectively making adjustments to the pressure exerted in the
processing area and the ozone gas volume supplied to the processing
area during an on-going cycle, and recycling and adjusting
wastestream volumes and any volumes of the cleaning fluid not
passing through the filter to be cleaned back to the processing
area, thereby reducing ozone bubbles and white water therefrom in
the wastestream and cleaning fluid as it is directed in the system
of conveyance from within the processing area to the filter
installation to be cleaned; wherein said method further comprises
generating an effluent portion volume after the forward entry and
passage through the filter installation to be cleaned of the
homogeneous cleaning fluid, said effluent portion volume being
equal to from about 25 percent to about 30 percent of the
respective volume of the waste stream from the respective source
area of the wastestream..Iaddend.
.Iadd.76. The method of claim 23, wherein the pressure gradient is
brought about by an ozone generator at an output of at least from
about 1 p.s.i.g. to about 150 p.s.i.g..Iaddend.
Description
BACKGROUND OF THE INVENTION
1. Field of the Invention
The present invention relates to the use of ozone to treat and
process aqueous waste feedstream, especially as this would relate
to treatment at filtration plant facilities; but also in other
uses, where the concern or object exists to improve flux rates of
feedstream through filter media and effectively change feedstream
character so that it is presented in a condition where it will
cause less wear or destruction of such media, and provide the added
feature of effectively cleaning such filter media.
2. Background Information
It has been determined in the art that Ozone kills many biological
agents by oxidizing the organic molecules that form the cell
surface and in dealing with the problem of calcium buildup (a major
portion of total dissolved solids--TDS), as well as dealing in the
past with biocides used to chemically treat water systems.
Those references found which appear to have at least some
relationship to the technology of ozone treatment and processing of
environmentally significant aqueous waste feedstream including the
fllowing: Williams, et al., U.S. Pat. No. 6,183,646; Crisinel, et
al., U.S. Pat. No. 6,162,477; Foellmi, U.S. Pat. No. 6,074,564;
Shultz, U.S. Pat. No. 6,001,247; Faivre, et al., U.S. Pat. Nos.
5,843,307 and 5,271,830; Busch, Jr., U.S. Pat. No. 5,807,486;
Tempest, Jr., U.S. Pat. No. 5,741,416; Bhave, et al., U.S. Pat. No.
5,645,727; Dickerson, U.S. Pat. No. 5,397,480; Ditzler et al., U.S.
Pat. No. 5,114,576; Engel et al., U.S. Pat. No. 5,097,556; Cole, et
al., U.S. Pat. No. 4,849,115; Hiltebrand, et al., U.S. Pat. No.
4,622,151; Cohen, et al., U.S. Pat. No. 4,595,498; and Johnson, et
al., U.S. Pat. No. 4,200,526.
Also having some relevance in terms of discussing some of the
chemical principles involved in the present invention's technology
(such as solubility aspects, pressure and the application of the
Laws of Boyle, Charles, Dalton and Henry, and other chemical
aspects), are the following references: (1) Various editions of
Lange's Handbook of Chemistry, setting forth the "Solubility of
Gases in Water," particularly as this relates to Oxygen and Air
into Water or Water and Solvents; (2) Graik, et al., 2001, "The
Effect of Ozone Gas-Liquid Contacting Conditions in a Static Mixer
on Microorganism Reduction," Ozone Science & Engineering, Vol.
23, pp. 91-103; (3) Min Cho et al., 2001, "Effect of pH and
Importance of Ozone initiated Radical Reactions In Inactivating
Bacillus subtilis Spore," Ozone Science & Engineering, Vol. 24,
pp. 145-150; (4) Mortimer, C. H., 1981, "The oxygen content of
air-saturated fresh waters over ranges of temperature and
atmospheric pressure of limnological interest," International
Association Of Theoretical And Applied Limnology, pp. 1-23, E.
Schweizerbart'sche Verlagsbuchhandlung: Stuttgart; (5) Langlais, et
al. (eds.), 1991, Ozone In Water Treatment Application and
Engineering, pp. 90-132, 349-442, 474-485 and 543-551; (6)
Masschelein, W. J. (ed.), 1982, Ozonization Manual for Water and
Wastewater Treatment, pp. 47-56, 69-102, 129-139, and 151-153, John
Wiley & Sons: New York; (7) Gerrard, w\W., 1976, Solubility Of
Gases and Liquids, pp. 1-276, Elsevier Scientific Publishing
Company: New York; (9) Lide, D. R. (ed.), 1995-1996, "Vapor
Pressure Of Fluids At Temperatures Below 300K--Ozone (O.sub.3)",
CRC Handbook of Chemistry and Physics, p. 6-71, CRC Press: New
York; and (10) Linke, W. F., 1965, "O.sub.3 Ozone Solubility In
Water," Solubilities Inorganic and Metal-Organic Compounds, pp.
1239-1240, American Chemical Society: Washington, D. C.
The Faivre et al. '307 and '830 patent references would appear to
be the closest potentially applicable prior art. The '307 reference
is entitled: "Unit for the treatment of water by ozonation, and a
corresponding installation for the production of ozonized water."
The '830 reference is entitled: "Water treatment installation for a
tangential filtration loop." These references teach a water
treatment unit and installation designed expressly for the purpose
of producing "ozonated white water," or water characterized by a
multi-phase, non-homogeneous mixed system containing gaseous
"bubbles" of ozone within the water, giving the water the
appearance of turbulent `white` water, and disclosed to have
bubbles the size of between 20 and 200 microns, or larger in
magnitude by virtue of the visibility to the naked eye of bubbled
white water as described in Faivre.
The bubbles and white water of the Faivre teachings are designed to
create physical turbulence in the water at the membrane, and employ
the ability of ozone, in such a gaseous state, as an oxidation
agent to further restrict clogging of their tangential filtration
membrane. Such installations or units require a reduction in
initial pumping pressure to form gaseous ozone bubbles, and a phase
separation to prevent cavitation of pumping units and other
equipment on line by virtue of Faivre's feedstream being at a point
of supersaturation with the presence of potentially damaging
gaseous bubbles; therefore, exposing such a system to the loss of
useful ozone content, even in the form of the gas bubbles earlier
created, as well as further time and expense in reinstating gaseous
ozone bubble concentrations with regard to any recycling
operations. The pressure in the Faivre installation must be dropped
some 50% to 75% before reaching any filter unit to form Faivre's
ozone gas bubbles. The unit or installation system of Faivre cannot
sustain useful pressure throughout its system loop, from beginning
to end, during any given cycle of its application or operation.
This loss in pressure will decrease potential flow rate across
tangential membranes along with significant reduction in
turbulence. Nor can it recycle, as indicated, without losing its
gaseous `white water-bubbled ozone and starting from the beginning
in re-generating its gaseous ozone bubbles or white water. These
systems, therefore, lose their ability to effectively clean filter
media because gaseous bubbled ozone, multi-phase fluid or
suspension is submitted not to be an optimal form for effectively
cleaning and saving wear on filter media. Nor is it effective and
cost-saving in re-utilization through re-cycling because of the
required reduction in pressure to form ozone bubbles and the phase
separation required to protect against cavitation and other phase
separation damage to pumps and other such equipment within Faivre's
loop, or other equipment utilized on-line. This is born out by its
relative or substantial obscurity of use in any environmental
system employing filter media in the United States. Additionally,
the teachings of Faivre would suggest, chemically, that its unit,
installation or system, is sensitive to temperature and pH
requirements because of the nature of its gaseous multi-phase
mixture; thereby inherently involving greater potential for failure
or demanding greater time and expense to maintain.
These and other disadvantages, structurally, functionally and by
virtue of distinction in process and method approach, will become
apparent in reviewing the remainder of the present specification,
claims and drawings.
Accordingly, it is an object of the present invention to provide a
substantially improved and cost-effective method in treating
aqueous waste feedstream for improving the flux rates, cleaning and
prolongation of useful life of filter media in many diverse
environmental and process applications; with special adaptability
and advantageous application to aqueous feedstreams from nuclear
plant sites.
It is a further object of the present invention to provide a method
which utilizes the solubilizing (or the making soluble and uniform)
of an ozone mixture (provided as having at least O.sub.3 and
O.sub.2) and an aqueous feedstream to create a substantially
homogeneous single phase liquid mixture or a substantially
homogeneous molecular single phase mixture, without `white water`
or ozone bubbles; so that the ozone mixture generated within the
present process and the aqueous feedstream to which it is applied
are dissolved and miscible, one with the other, at a level below
the saturation point of the generated ozone mixture (rather that at
point of supersaturation); thus making it a more active and
concentrated ozone solution system (with greater oxidizing power
and cleaning ability).
It is yet a further object to provide a system and process of
dissolving and solubilizing ozone in an aqueous feedstream to
produce a substantially single phase liquid system which will not
damage filter media, pumps and like units on-line; and which can be
maintained at a desired or higher pressure throughout the system
on-line, from the beginning to the end of a complete given cycle,
for maximizing the positive effect of the concentrated active
oxidation or oxidizing power of such a single phase liquid system
on a filter media; through enhanced cleaning, improved flux rates,
improved quality and volume amount of effluent permeate, and the
ability to recycle reject volumes for further cleaning and
oxidation exposure without having to lower the pressure
on-line.
It is a further object of the present invention to provide a
solubilized ozoneaqueous feedstream system which will have greater
ozone concentration and oxidation activity at the surfaces of
filter membranes or other filter media surfacing, for improved
cleaning and prolonged useful life; while also serving functionally
to cost-effectively facilitate greater amounts of permeate, faster
re-cycling rates and greater volume movement potential throughout
the system in relation to time.
It is yet a further object of the present invention to provide a
method and system which will operate well at various pH and
temperature ranges or ambient conditions at a given site.
It is an additional object of the present invention to sustain a
workable higher pressure above atmospheric pressure throughout the
on-line system and installation constituted in accordance with the
present invention, to achieve the most optimal concentration and
resulting activity of ozone in solution with an aqueous feedstream
so that the full advantages of utilizing ozone to clean and prolong
the life of otherwise expensive filter media are realized in that:
(1) Since ozone is generated by an electrical discharge into oxygen
(supplied as plant air), no handling of hazardous chemical is
required, with a flip of a switch beginning ozone production; (2)
Ozone has a much higher oxidation potential than hypochlorite (free
chlorine) or hydrogen peroxide, which means that it reacts faster
and attacks organics at a much higher rate; (3) Ozone decomposes to
oxygen, so no chemical contaminants (e.g., sodium chloride or
chloramines) will affect downstream ion exchange performance or
capacity; (4) Ozone has a half-life of approximately 20 to 30
minutes, so there is no credible scenario for it to be found in
plant effluent; and (5) Ozone dissolved in water is less aggressive
to Tubular Ultra Filtration, Cross-Flow Membrane Media or other
filtration means or units than hypochlorite or like chemicals or
substances. Therefore, the use of ozone can enhance membrane life
and reduce membrane fouling and frequency of cleaning, while
maintaining a higher flux rate.
It will, therefore, be understood that substantial and
distinguishable process and functional advantages are realized in
the present invention over the prior art; and that the present
invention's efficiency and adaptability of operation, diverse
utility, and broad functional applications serve as important bases
of novelty and distinction in this regard.
SUMMARY OF THE INVENTION
The foregoing and other objects of the invention can be achieved
with the present invention, method, process and system which is a
method and system for processing organic pollutants, and inorganic
foulants in a reduced oxidative state, of an aqueous feedstream,
for increasing flux rates across a filtration membrane, and for
cleaning and prolonging the useful life of filtration and filter
membrane installations.
The method and system of the present invention is provided with
step (a) which includes: directing, channeling and pumping an
aqueous feedstream having waste contaminants, from a feed water
area to a reactor area for contacting, reacting, pressurizing and
equalizing the aqueous feedstream, and concentrating solids and
removing solids from the aqueous feedstream.
The method is further provided with step (b): generating an ozone
mixture having at least O.sub.3 and O.sub.2, dissolving the ozone
mixture into the aqueous feedstream under a pressure gradient
having an alpha pressure, contacting the aqueous feedstream with
the ozone mixture such that the aqueous feedstream is exposed for
increased reaction of the ozone and concentrating and collecting
solids at a bottom portion of the processing area.
Step (c) of the present invention includes: directing the aqueous
feedstream from the reactor area and measuring ozone activity of
the aqueous feedstream.
Step (d) includes: conveying the aqueous feedstream to a pumping
area.
Step (e) comprises: pumping the aqueous feedstream to a filtration
area having filter media, an inflow portion subarea and an outflow
portion subarea, respectively, before and after the filter
media.
Step (f) of the present method and system of the invention
includes: marshaling an effluent portion volume of the aqueous
feedstream passing through the filter media of the filtration area
to the outflow portion subarea, and advancing and measuring ozone
activity of the effluent portion volume, and the volume and amount
of the effluent portion volume; and
Step (g): advancing the effluent portion to a preselected site.
BRIEF DESCRIPTION OF THE DRAWINGS
FIG. 1 is an exemplar flow diagram and schematic illustration of a
preferred embodiment of the novel and substantially improved method
in treating aqueous waste feedstream for improving the flux rates,
cleaning and useful life of filter media of the present
invention.
FIG. 2 is an exemplar flow diagram and schematic illustration of
another preferred embodiment of the present invention.
FIG. 3 is another exemplar schematic, diagrammatic illustration of
an embodiment related to that illustrated in FIG. 2.
FIG. 4 is an exemplar schematic diagram illustrating one of the
preferred embodiments of the Reactor Area of the embodiment of the
present invention illustrated in FIG. 1.
FIG. 5 is an exemplar schematic, diagrammatic illustration of
another preferred embodiment of the Reactor Area utilized in the
embodiment of the present invention illustrated in FIG. 1.
.Iadd.FIG. 6 is an exemplar schematic, diagrammatic illustration of
preferred embodiment of the present invention related to that of
FIG. 1..Iaddend.
REFERENCE NUMBERS
10 Ozone method (Present Method System or Installation) 11 aqueous
waste feedstream (or aqueous feedstream from 14) 14 plant or site
waste water source area 16 Reactor Area 18 feed control valve (or
equalizer volume-amount valve or tank equalizer) 20 O.sub.3/O.sub.2
mixture (ozone mixture) alpha pressure at which feedstream is
pumped into Reactor Area (16) and Reactor (72) in preferred
embodiments of the invention 16A temporary or intermediary upper
area of (16) (FIG. 4) 16B temporary or intermediary lower area of
(16) (FIG. 4) 16C top portion of (16) (FIG. 5) 16D lower portion
(16) (FIG. 5) 30 .Iadd.ozone measurement or ORP .Iaddend.sensor
area 32 pumping area 40 filtration area 42 filter media (filter
membrane) 44 inflow side portion subarea 46 outflow side portion
subarea 50 effluent permeate portion volume 52 .Iadd.ozone
measurement or ORP .Iaddend.sensor area 60 reject portion volume 62
recycle line (recycle reject line) 64 .Iadd.ozone measurement or
ORP .Iaddend.sensor area 70 dissolving area 72 Reactor (another
preferred embodiment)(FIGS. 2 and 3) 74 Recycle Tank (FIGS. 2 and
3) 76 .Iadd.ozone measurement or .Iaddend.ORP sensor 78 back
pressure valve (BPV) 80 ozone .Iadd.measurement .Iaddend.or ORP
sensor 82 Recycle booster pump 83 recycle line 84 further back
pressure valve 86 further ozone .Iadd.measurement .Iaddend.or ORP
sensor
DETAILED DESCRIPTION OF THE PREFERRED EMBODIMENTS OF THE
INVENTION
The following description of the preferred embodiments of the
concepts and teaching of the present invention is made in reference
to the accompanying drawing figures which constitute illustrated
schematic examples of the methodical, systematic and functional
elements of the present invention, among many other examples
existing within the scope and spirit of the invention.
Referring now to the drawings, FIGS. 1, 2 and 3, thereof, there is
diagrammatically illustrated an ozone method, process, installation
and system in treating aqueous waste feedstream for improving the
flux rates, cleaning and the prolongation of the useful life of
filter membrane units and filter media .[.10.]. .Iadd.42.Iaddend.,
of the present invention; referred to hereinafter as the Ozone
Method (or Present Method or System) 10.
.Iadd.As indicated, hazardous chemicals and substances can be
involved in dealing with aqueous waste feedstreams associated with
a manufacturing plant, nuclear plant site or other facility
producing aqueous waste having organic or inorganic pollutants and
foulants; regarding which the present invention process is
directed. The U.S. Environmental Protection Agency's (EPA's)
regulations establish two ways of identifying solid wastes as
hazardous under the RCRA (Resource Conservation and Recovery Act,
enacted in 1976). A waste may be considered hazardous if it
exhibits certain hazardous properties ("characteristics") or if it
is included on a specific list of wastes EPA has determined are
hazardous ("listing" a waste as hazardous) because the EPA found
them to pose substantial present or potential hazards to human
health or the environment. EPA's regulations in the Code of Federal
Regulations (40 CFR) define four hazardous waste characteristic
properties: ignitability, corrosivity, reactivity, or toxicity (see
40 CFR 261.21-261.24). For example, an aqueous waste feedstream
associated with a nuclear plant site can and often does include
"corrosion products" or corrosion materials (See, for example, EPA
referenced publications: Gorby, Y. A., G. G. Geesey, F. Caccavo,
Jr., AND J. K. Fredrickson, MICROBIALLY PROMOTED SOLUBILIZATION OF
STEEL CORROSION PRODUCTS AND FATE OF ASSOCIATED ACTINIDES. Pacific
Northwest National Laboratory, Richland, Wash., 2000 and Ewing, R.
C., "Corrosion of Spent Nuclear Fuel: The Long-Term Assessment",
Federal Annual Grant Report (Sep. 15, 2000 to Jun. 15, 2001),
Environmental Management Science Program, Univ. of Michigan.
Other criteria for hazardous wastes are set out in 40 CFR Part 266
and other related statutes and regulations. Also set forth in this
regard are requirements for verification by various forms of
representative testing or sampling. See, for example: Environmental
Protection Agency (EPA). 1980b. Samplers and Sampling Procedures
for Hazardous Waste Streams, EPA-600/2-80-018, EPA, Washington,
D.C. (PB80-135353).
Terms utilized herein, or implied by their common understanding by
those skilled in the art, have been defined by their conventional
definitions, as set forth by standard dictionary/glossary and EPA
or USGS references known by, or readily accessible to, those
skilled in the art, for example, as follows: contaminant--A
substance in water of public health or welfare concern. Also, an
undesirable substance not normally present, or an unusually high
concentration of a naturally occurring substance, in water, soil,
or other environmental medium. Contamination of water involves
impairment of the quality of water sources by industrial waste or
other matter. pollutant--Something that pollutes, especially a
waste material that contaminates air, soil, or water. Any substance
of such character and in such quantities that when it reaches a
body of water, soil, or air, it is degrading in effect so as to
impair their usefulness or render them offensive. Any solute or
cause of change in physical properties that renders water unfit for
a given use. pollution--Any alteration in the character or quality
of the environment which renders it unfit or less suited for
certain uses. With respect to water, the alteration of the
physical, chemical, or biological properties by the introduction of
any substance that adversely affects any beneficial use. Under the
Clean Water Act (CWA), for example, the term is defined as the
manmade or man-induced alteration of the physical, biological,
chemical, and radiological integrity of water. wastewater--A
combination of liquid and water-carried pollutants from homes,
businesses, industries, or farms; a mixture of water and dissolved
or suspended solids. hazardous material, waste or chemical is a
substance, pollutant or contaminant listed as hazardous under the
Comprehensive Environmental Response, Compensation, and Liability
Act (CERCLA) of 1980, as amended, and the regulations promulgated
pursuant to that act. Hazardous Substance is any material that
poses a threat to human health and/or the environment. Typical
hazardous substances are toxic, corrosive, ignitable, explosive, or
chemically reactive. Any substance designated by the U.S.
Environmental Protection Agency (EPA) to be reported if a
designated quantity of the substance is spilled in the waters of
the United States or if otherwise released into the environment.
Water Words Dictionary, NEVADA DIVISION OF WATER PLANNING,
published with all supporting references prior to 2001, and cited
and referenced by the USGS Water Science Glossary of Terms.
foulant: the accumulation of undesirable foreign matter in a filter
or ion exchange media bed causing clogging of pores or coating of
surfaces and inhibiting or limiting the proper operation of the bed
and the treatment system; and a phenomenon in which a reverse
osmosis or ultrafiltration membrane adsorbs, interacts with, or
becomes coated by solutes and/or precipitates in the feed stream
resulting in a decrease in membrane performance by lowering the
flux and/or affecting the rejection of solutes. (WQA) Glossary of
Terms, Glossary Reference 1999, Water Quality Association, Lisle,
Ill. organic matter--Chemical substances of animal or vegetable
origin, or more correctly, of basically carbon structure,
comprising compounds consisting of hydrocarbons and their
derivatives. conventional pollutants: Statutorily listed pollutants
understood well by scientists. These may be in the form of organic
waste, sediment, acid, bacteria, viruses, nutrients, oil and
grease, or heat. dissolved solids: Disintegrated organic and
inorganic material in water. Excessive amounts make water unfit to
drink or use in industrial processes. grab sample: A single sample
collected at a particular time and place that represents the
composition of the water, air, or soil only at that time and place.
A Sampler is a device used with or without flow measurement to
obtain a portion of water or waste for analytical purposes. oils
and grease is a common term used to include fats, oils, waxes, and
related constituents found in wastewater. Grease, itself, in
wastewater, involves a group of substances including fats, waxes,
free fatty acids, calcium and magnesium soaps, mineral oils, and
certain other nonfatty materials. EPA Terms of Environment
Glossary, Abbreviations, and Acronyms, EPA 175-B-97-001 (Revised
December, 1997); Environmental Engineering Dictionary and
Directory, Pankratz, T. M., Lewis Publishers, 2001; and GLOSSARY
WATER AND WASTEWATER CONTROL ENGINEERING (Ed., Ingram, W. T., et
al., Water Pollution Control Federation et al., 1969. Inorganic
contaminant (IOC): An inorganic substance regulated by the US
Environmental Protection Agency in terms of compliance monitoring
for drinking water. Contained on the agency's list are contaminants
as diverse as asbestos, nitrate (NOsub.3.sup.-), cyanide, and
nickel. An inorganic contaminant is sometimes called an inorganic
chemical. Mineral-based compounds such as metals, nitrates, and
asbestos. These contaminants are naturally-occurring in some water,
but can also get into water through farming, chemical
manufacturing, and other human activities. EPA has set legal limits
on 15 inorganic contaminants. Inorganic waste includes discarded
material such as sand, salt, iron, calcium, and other mineral
materials. monitoring: Testing that water systems must perform to
detect and measure contaminants. A water system that does not
follow EPA's monitoring methodology or schedule is in violation,
and may be subjected to legal action. organic contaminants:
Carbon-based chemicals, such as, for example, solvents and
pesticides, which can get into water through runoff from cropland
or discharge from factories. EPA has set legal limits on 56 organic
contaminants. sample: The water that is analyzed for the presence
of EPA-regulated drinking water contaminants. Depending on the
regulation, EPA requires water systems and states to take samples
from source water, from water leaving the treatment facility, or
from the taps of selected consumers. corrosion: The dissolution and
wearing away of metal caused by a chemical reaction such as between
water and the pipes, chemicals touching a metal surface, or contact
between two metals. The Drinking Water Dictionary, (Ed. Talley, D
et al.), American Water Works Association, 2000; Ground Water &
Drinking Water--Drinking Water Glossary and A Dictionary of
Technical and Legal Terms Related to Drinking Water, EPA
Publications; and EPA Terms Of Environment Glossary, Abbreviations,
and Acronyms, EPA 175-B-97-001 (Revised December, 1997 and as
updated)..Iaddend.
The Ozone Method 10 is utilized for environmentally processing
organic pollutants and inorganic pollutants (or foulants) having or
characterized chemically by a reduced oxidative state, which are
part (or part and parcel) of an aqueous waste feedstream associated
with a manufacturing, plant, nuclear plant site or other facility
producing aqueous waste.
The Present Method 10 is utilized to increase flux rates across a
filtration membrane.Iadd., .Iaddend..[.(or filter media).].
.Iadd.or other filter installation.Iaddend., for cleaning such a
membrane .Iadd.media .Iaddend.or .[.media.].
.Iadd.installation.Iaddend.; and for prolonging and extending the
useful operative life of such .[.filter media.]. .Iadd.filtration
systems.Iaddend.. These useful applications apply to many diverse
types of filter media.[., and.]. .Iadd.and installations, but
.Iaddend.have been found to work well with cross-flow filter media
and tubular membrane media.[.,.]. over a wide range of pH values
and temperatures (with 50 to 140 degrees F. being preferred when
ambient conditions permit).
The Ozone Method 10 is provided with the initiating step of
directing, channeling and pumping an aqueous waste feedstream,
shown generally at 11 (and as a line passing through the present
system), having waste contaminants from a plant or site waste water
source area 14 associated with a plant or other facility; to a
Reactor Area 16, shown by example in FIGS. 1, 4 and 5.
Additionally, the site waste water source area 14 can, in fact, be
any body of aqueous liquid or fluid which is the subject or target
of cleaning, purifying or a filtration process. Many aqueous food
liquids, solutions or fluids such as juice, soups and other foods
could be included, as well as any aqueous body to be cleaned. The
Reactor Area 16 is utilized in the method and system of the present
invention and installation for the purpose of contacting, reacting,
pressurizing and equalizing (on re-cycle) the aqueous feedstream 11
passing through the Present System 10; and for concentrating solids
within the aqueous feedstream 11. The feedstream 11 is
diagrammatically illustrated as passing through the illustrated
method and system diagram or flow chart, and will be understood by
those skilled in the art. The Reactor 16 is provided as a tank,
vessel, container, receptacle or reservoir which can function with
pressures above 2000 PSIG. (pounds per square inch, gauge, versus
absolute pressure, also shown herein by the designation "p.s.i.g.")
in magnitude.
The aqueous feedstream 11 is taken from a .[.plant waste water site
16.]. .Iadd.plant or site waste water area 14 .Iaddend.and pumped
at a pressure (referred to herein as the alpha pressure) of from
about 10 to about 150 PSIG (or higher), or a preferred range of
from about 30 to 50 PSIG (depending on the qualitative and
quantitative nature of the feedstream 11) to a feed control (or
equalizer-volume-amount tank) valve 18 (or gauge); and then to the
Reactor 16. It will be understood within the scope and spirit of
the present invention that the valve or gauge 18 can be positioned
or installed with a positional orientation outside of, within
and/or adjacent or beside the Reactor 16. The use of much higher
alpha pressures of 100 PSIG to 2000 PSIG can be employed, as
indicated, with regard to, and use of, some of the newer filter
media becoming available in this technology.
The valve 18 is utilized initially to meter, measure or quantitate
a selected or preselected volume or amount of aqueous feedstream
11; and will generally (depending on the site) have a starting
amount of, for example, about 300 to 400 gallons (or equivalent
volume) of feedstream 11. It will be understood within the scope of
the present invention that this volume or amount can also be less
or considerably more. This amount of aqueous feedstream 11 will,
therefore, be directed, channeled, piped or otherwise conveyed, at
the alpha pressure (or under the alpha pressure gradient), and at
this higher pressure above atmospheric pressure, into the Reactor
Area 16. It will be understood that one (1) atmosphere of pressure
(760 mmHg., 1.103 bar) is equal to about 14.70 lbs. per square inch
(p.s.i).
The valve 18 is further utilized after a cycle in the present
system 10 is completed, as further described below, to meter or add
in an amount or volume of additional feedstream 11 from the plant
waste water source area 14 equal or equivalent in volume or amount
to the volume or amount extracted at the end of a given cycle as
effluent permeate, later described herein; therefore restoring the
feedstream (or recycled remaining feedstream) to its original
starting amount or volume (as indicated by example earlier as, for
example, 300-400 gallons, but which will vary in accordance with
starting conditions).
A mixture containing at least O.sub.3 and O.sub.2 (ozone and
diatomic oxygen, recognizing that molecular oxygen is O.sub.2 and
ozone is O.sub.3) is generated by an ozone generator utilizing air
or an O.sub.2 source (such as an oxygen separator); and the
O.sub.3/O.sub.2 mixture 20 is educted, causing a partial vacuum and
thus drawing the O.sub.3/O.sub.2 mixture 20 into the Reactor Area
16. It will be understood within the scope of the invention that
the mixture 20 can otherwise be generated, conveyed and supplied to
the Reactor 16. Many ozone generators are available on the market
which can be utilized in this part of the process. An example, of
many such generators which are employable or adaptable for use,
includes the Model 1250 Ozone Generator made by CEC, 2749 Curtiss
Street, Downers Grove, Ill. 60615. Many other types and models of
ozone generators, and other equipment creating, forming or
generating ozone mixtures 20 can be utilized satisfactorily within
the present method and system installation 10.
Examples, without limitation, of ozone generator use parameters
include the following specification: Design Pressure: 150 PSIG;
Design Temp: 150 degrees F.; Design Feed Stock: Radioactive Waste
Water; Designed TOC Destruction Rate: 300 ppm-gpm; Hydrostatic Test
Pressures: 1.5.times. Design Pressure; Maximum Allowable Feed
Pressure: 150 PSIG; Typical Feed Pressure 50 to 100 PSIG; Maximum
Allowable Operating Pressure: 50 PSIG; Nominal Operating Pressure
30 to 45 PSIG; Max. Allowable Operating Effluent Press.: 50 PSIG;
Nominal Operating Effluent Press.: 30 to 45 PSIG; Max. Allow.
Operating Temp.: 140 degrees F.; Min. Allow. Oper. Temp.; 32
degrees F.; Nominal Oper. Temp.: 50 to 104 degrees F.; Nom. CIP
Oper. Temp.: 60 to 135 degrees F.; Peak Flow Rate: 50 GPM; Typical
Flow Rate 15 to 40 GPM; and Min. Flow Rate: 5 GPM.
The feedstream 11 is, therefore, pumped into the Reactor 16 at the
alpha pressure, for example between 30 to 50 PSIG (or higher), and
the ozone mixture 20 is generated and provided to the Reactor 16
and dissolved into the aqueous feedstream 11 so that the mixture 20
is solubilized (or made soluble) within and with the aqueous
feedstream 11, to produce a substantially or generally homogeneous
single phase liquid mixture, where the ozone mixture 20 in the
aqueous feedstream is dissolved and miscible, one with the other,
in a consistent liquid solution without the presence of bubbles or
any white water created by ozone bubbles; and where the ozone
mixture 20 is dissolved in the aqueous feedstream at a level below
the saturation point of the ozone mixture 20. The elevated pressure
of the Reactor 16, because of the alpha pressure that the
feedstream is pumped in at, improves the rate and equilibrium of
the solubility of the ozone mixture 20 and the feedstream 11 in the
Reactor 16. It will also be understood within the scope of the
invention that a pressure gradient can be brought to bare on, or
established in, the Reactor 16 through means other than the
pressure at which the feedstream 11 is pumped into the Reactor.
Additionally, within the Reactor Area 16, the aqueous feedstream
11, now containing and being dissolved with the ozone mixture 20
(O.sub.3 and O.sub.2), is exposed to physical surfacing or
additional surface opportunities, so that further oxidation or
oxidizing reaction can take place by virtue of the effect that the
concentrated and dissolved ozone has on the ingredients and
pollutants of the feedstream 11; and improved Ozonalysis can take
place. Examples within the scope and spirit of the invention which
set forth, in exemplar preferred embodiments how the contacting and
additional surfacing opportunities can be achieved include those
illustrated in FIGS. 4 and 5.
FIG. 4 illustrates a Reactor Area 16 where the aqueous feedstream
11 is provided to the Reactor 16 from piping or channeling which
leads to a nozzle member 22 supported within the Reactor 16 for
conveying and spraying the feedstream 11 to a temporary or
intermediary upper area 16A within the Reactor 16 which initially
contains the ozone mixture 20 provided to the Reactor 16.
Initially, or during the initial stages or sequences of time during
which the feedstream 11 and the ozone mixture 20 enter the Reactor
16, the feedstream 11, because of the initial effect of its
density, will drop to the temporary or intermediary lower area 16B;
contemporaneously or shortly followed by the effect of the alpha
pressure gradient which is established in the Reactor 16,
facilitating the mixing and solubilizing earlier discussed. This
permits greater contact, surface exposure and reaction potential;
and, therefore, greater oxidizing opportunities, between the
feedstream 11 and the ozone mixture 20.
Another example of accomplishing the contacting, mixing and
reaction functions of the Reactor area 16 of the present invention
is illustrated in FIG. 5. In this preferred embodiment the aqueous
feedstream 11 is provided initially to a top portion 16C of the
Reactor 16 so that it substantially or generally fills the area 16
(with some space left at the top as illustrated). The ozone mixture
20 is provided to a lower portion 16D (or spaced portion in
relation to the position of the top surfacing of the feedstream or
the space left where the area 16 is not completely filled),
directly into the feedstream 11; and permitted initially (or in an
intermediary sequence) because of the lower density of the gas, as
initially provided, to rise through the body of the feedstream 11
from the area 16D to the top or upper portion, while or until the
alpha pressure gradient has its effect in homogeneously
solutionizing or solubilizing the ozone mixture 20 within the
feedstream 11. This embodiment of the present method 10 permits
greater opportunity for surfacing (or providing or exposing more
surface area) and contacting; and, therefore, provides more
opportunities for further oxidation reactions between the ozone of
the mixture 20 and the pollutants (organic and inorganic) of the
aqueous feedstream 11 to occur. It will be understood within the
scope of the present invention that other means of contacting and
surfacing the mixture 20 and the feedstream 11 can be utilized,
such as passing them over or through various columns or packed
columns, etc., for exposing the feedstream 11 to further angles and
surfaces of dissolving and reaction with the ozone contained in the
ozone mixture 20.
Also included within the activities and functions within the
Reactor 16 of the present ozone method 10 is a concentrating and
relegation (location or positional orientation) of solid substances
(compounds or materials) to a bottom area of the Reactor 16 for
removal during a preselected sequence of time during the operation
or cycling of the method 10; as shown schematically, by example, in
FIGS. 1, 2 and 3.
The present method 10 further includes directing the ozone
dissolved, feedstream 11 from the Reactor Area 16, after the
process discussed above, to a sensor area 30, where the ozone
activity of the feedstream 11 is measured. This activity is
commonly measured, within preferred embodiments of the invention,
as an analysis of ozone content (such as.Iadd., for example,
.Iaddend.by virtue of a titration indicator means) within the
feedstream 11, or as.Iadd., for example, .Iaddend.an ORP (oxidation
or oxygen reaction potential, or redox potential). For example, an
ORP reading of +500 mV or above, indicates an extensive ozone
oxidizing condition; one indicating a non-foulant (or non-polluted)
state, character or feedstream condition. Positive values in this
respect could run within a target range of from about +500 mV to
about +1000 mV; with the solubility limit of ozone being
characterized by a value of +1400 mV; and a condition where the
feedstream had little or no ozone content being characterized by an
ORP value of less than about +100 mV. It is, therefore, one
important feature and novelty of the present method 10 that the ORP
value is adjusted in a positive manner; to, therefore, indicate
positive adjustment increase and substantially improved
effectiveness of ozone concentration. Various ozone or ORP sensor
areas (as illustrated by example in the drawings) are, therefore,
provided along the on-line cycle of the present method and
installation 10 to assure that this positive ozone concentration
(and denoting positive ORP reading) is taking place; and to make
positive adjustments (within a cycle or upon re-cycle) if this is
not, for some reason, taking place. .Iadd.Ozone content is normally
measured by various sampling methods known in the art or described
or mandated by the EPA; and ORP readings, as indicated by example
above are determined by sensor or primary element means among other
sensor means for verifiability measuring the ORP
content..Iaddend.
In a preferred embodiment of the method 10, the data obtained in
ORP units at the sensor 30 is utilized on recycle of the process to
adjust the output or production of ozone concentration from an
ozone generator utilized to an amount which will render the
feedstream and dissolved ozone mixture leaving the Reactor Area 16
at an ORP value of from about 750 mV to about 800 mV.
The present method 10 further, then, includes conveying the
feedstream 11 to a pumping area 32, and pumping the feedstream 11,
while maintaining the alpha pressure, to a filtration area 40,
characterized and illustrated herein as having the filter media 42
(or filter membrane), the inflow side portion subarea 44 and the
outflow side portion subarea 46; as illustrated in FIGS. 1, 2 AND
3. And, as so characterized, the filter 42, the inflow side 44 and
the outflow side 46 are positioned, respectively, in the middle
(indicated by a diagonal line), in front of (or positioned before
the middle), and behind (in back of, after or following) the middle
of the filtration area 40, as illustrated.
It will be understood within the scope .Iadd.and spirit .Iaddend.of
the present method and installation 10 of the invention that a
number of different pumps.Iadd., channeling or directing devices,
systems and means .Iaddend.can be utilized in the pumping
area.Iadd., or directing or channeling means area .Iaddend.32; and
that the present invention is applicable to cleaning.[.,.].
.Iadd.and .Iaddend.improving the flux rate.Iadd., .Iaddend.and
prolonging the useful life (from 2 to 5 years longer) of various
types of filtration units .Iadd.or installations
.Iaddend.(illustrated schematically as the filtration area 40). For
example, the method 10 is especially useful in relation to cross
flow filtration and tubular system filtration units .Iadd.or
installations .Iaddend.employed at manufacturing plant and nuclear
waste site areas; but would be expected to improve the function,
capacity and working time of any type of filtration or filter
membrane system.Iadd., installation, .Iaddend.or other type.[.s.].
of filter or cleaning system.[.s.]. utilized in relation to
processing.Iadd., or interacting with, .Iaddend.an aqueous waste
feedstream.
An example of one such system with which the present method 10 can
be used is the A19 Ultrafiltration System (PCI Membrane Systems 19
tubular UF/MF System) manufactured by PCI Membrane systems Limited,
Laverstoke Mill, Whitchurch, Hampshire RG287NR, UK. Many other
types of filter system or units including, but not limited to:
Filters used for Radioactive liquids; disposable filters; reusable
filters, precoat filters; septum filters; flatbed filters;
centrifugal filters; metallic, non- or partially-cleanable filters;
etched disk filters and miscellaneous filters (such as deep-bed
filters clam shell, magnetic, sand filters, etc.); can be
benefitted, or benefitted through adaptation, by the present method
10.
The present ozone method 10 further includes, in its installation
on-line system, marshaling (gathering and/or conveying), an
effluent permeate portion volume, shown generally at 50, from the
feedstream 11 after it has passed (or as it is passing) through the
filter media 42; designated in FIG. 1 as a permeate product; having
been affected to do so by the constant alpha pressure and the
oxidizing effect of the concentrated ozone in single phase solution
with the feedstream 11. This permeate 50 passes through the filter
media 42 to the outflow side portion subarea 46. The effluent
permeate 50 is then advanced to another sensor area 52, where it is
again measured for ozone activity, as discussed above. The
resulting volume and amount of effluent permeate 50; expected to be
from about 25% to about 30% of the original starting volume/amount
of the aqueous feedstream 11 (given above, by example, as 300-400
gallons); is also measured at this time; or is measured
contemporaneously in time in relation to recycling aspects of the
present method 10 discussed herein. In this regard, as discussed
above, the feed control valve 18 is utilized for the purpose of
adding back an amount of new feedstream from the waste water 14
equivalent or equal to the volume or amount of the permeate 50
derived and taken from the system as a product, prior to starting a
new cycle.
The effluent permeate 50 is then advanced to a selected or
preselected site or location for storage, use or further
conveyance.
The method 10 further includes marshaling of a reject portion
volume, generally indicated as 60, consisting of that part,
portion, amount or volume of the feedstream 11 not passing through
the filter media 42 and being positioned, by virtue of that fact,
at the inflow side portion subarea 44 of the filtration area 40;
and advancing the reject 60 to a continuation of the system
designated as a recycle line 62 (or recycle reject line).
The reject 60 is then conveyed to another sensor area 64 for
measuring the ozone activity of the reject 60, as discussed above
herein. The reject 60 is then channeled (conveyed or piped) back to
the Reactor Area 16 or the feed control valve 18 just outside,
within or a part of the Reactor Area 16, for metering, measuring
and addition of further restoration volumes or amounts of site
waste water 14 equal or equivalent to the amount of permeate
portion volume 50 taken out of the system as indicated above; thus
forming a new aqueous feedstream volume to be processed as
indicated in a re-cycle mode of the present method 10, and taken
through the same steps and process indicated above as a part of the
Method 10, for the purpose of obtaining further permeate product 50
while further cleaning the filter media 42.
Another preferred embodiment of the present method 10 of the
present invention is illustrated schematically in FIGS. 2 and 3. In
this preferred embodiment of the ozone method 10 the same processes
are carried out in accordance with the teachings of the present
invention set forth above. However, in this embodiment, at least
three (3) separate areas (such as tanks, vessels, containers,
reservoirs or cylinders) are utilized to address the steps and
parts of the present method 10.
In this respect, the Dissolving Area 70 is utilized to receive the
aqueous feedstream 11, pumped in under the alpha pressure from the
waste water area 14; and to mix and homogeneously dissolve the
ozone mixture 20 generated and provided to the area 70 with the
feedstream 11. The Reactor 72 is utilized to provide structure
and/or positionally arranged surfacing to expose the feedstream 11
to greater or increased oxidation by the ozone mixture 20 dissolved
in the feedstream 11. And the Recycle Tank 74 is utilized for
concentrating any solids forming a part of the feedstream 11 and
making them available for removal at a preselected time from the
Tank 74 and system 10.
An ORP sensor 76 is located, by preselected option, between the
waste water site 14 and the Dissolving Area 70. The Reactor 72 can
be optionally provided with packing material or other content or
positional orientations for providing greater surfacing potential
for the feedstream 11 passing through it.
A back pressure valve (BPV) 78 and an ozone or ORP sensor 80 are
provided on -line between the Reactor 72 and the Recycle Tank 74.
The valve 78 is utilized to maintain alpha pressure; and the sensor
80 is utilized as indicated to measure ozone activity.
A Recycle Booster Pump 82 is provided between the Recycle Tank 74
and the filtration area 40 for maintaining pressure and conveying
the feedstream through the filtration area 40, so that the reject
volume portions 60 are channeled to the recycle line 83 and the
permeate portions 50 are pumped through the filtration area 40 and
out of the system.
A further back pressure valve 84 and ozone or ORP sensor 86 are
provided on the recycle line 83. The recycle line 83 takes the
reject portion 60 back to the Recycle Tank 74 for further
processing as indicated in the original step and shown by schematic
flow-chart illustrated representation in FIGS. 2 and 3.
Accordingly, the appended claims are intended to cover all changes,
modifications and alternative options and embodiments falling with
the tree breath, scope and spirit of the present invention. The
reader is, therefore, requested to determine the scope of the
invention by the appended claims and their legal equivalents, and
not by the examples which have been given.
* * * * *
References